EP0213791B1 - Procédé pour la séparation d'huile brute - Google Patents

Procédé pour la séparation d'huile brute Download PDF

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Publication number
EP0213791B1
EP0213791B1 EP86306043A EP86306043A EP0213791B1 EP 0213791 B1 EP0213791 B1 EP 0213791B1 EP 86306043 A EP86306043 A EP 86306043A EP 86306043 A EP86306043 A EP 86306043A EP 0213791 B1 EP0213791 B1 EP 0213791B1
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Prior art keywords
tower
stream
crude
naphtha
pressure
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EP86306043A
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German (de)
English (en)
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EP0213791A2 (fr
EP0213791A3 (en
Inventor
Mahdevan Subramanian
David Johnson
Richard Monday
Frank Kleinschrodt
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Fluor Corp
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Fluor Corp
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils

Definitions

  • This invention relates generally as indicated to a process for separating crude oil components, and more particularly to such a process in which a preflash distillation tower operating at relatively high pressure is used.
  • atmospheric crude distillation units used for separating the desirable components of crude oil typically have an atmospheric crude tower, a naphtha splitter or naphtha stripper to separate the straight run naphtha into light straight run (LSR) naphtha and heavy naphtha, and several side strippers to produce components such as diesel, kerosene, and atmospheric gas oil.
  • LSR light straight run
  • side strippers to produce components such as diesel, kerosene, and atmospheric gas oil.
  • such atmospheric crude distillation units operate at near atmospheric pressure in order to evaporate all desirable components without exceeding cracking temperatures in the bottom of the crude distillation tower. This has led to the auxiliaries around the crude distillation tower being operated at about the same pressure as well.
  • the overhead product of the atmospheric crude tower either is a full range naphtha which is subsequently split into an LSR naphtha and a heavy straight run naphtha in a naphtha splitter, or the LSR naphtha is recovered as an overhead product of the atmospheric crude tower and the heavy naphtha is produced as the bottom product of a naphtha side­stripper connected to the atmospheric crude tower.
  • Previously known crude separation systems may include a preflash tower upstream of the atmospheric crude tower removing most of the not readily condensible components present in the crude oil charge, thereby reducing the load on the atmospheric crude tower.
  • Such preflash towers typically operate at pressure of less than 2.7 bar absolute (25 psig).
  • the present invention involves a process for separating the desirable components of crude oil that eliminates the off-gas compressor, separates the naphtha components more effectively and efficiently, does not suffer from the problems associated with water condensation and reduces the overall energy requirements.
  • US-A-3 320 159 describes a method of separating components of crude oil in accordance with the prior art portion of claim 1.
  • This prior proposal while working at a sufficiently high temperature to avoid water condensation in the distillation tower, only does this by use of a single tower for the complete distillation process.
  • the present invention as characterised in claim 1, uses the initial distillation tower simply for separating the more volatile components with the less volatile components being dealt with in the subsequent distillation unit.
  • the initial distillation tower instead of working at a compromise pressure, can work at a sufficiently high pressure as to avoid repressurisation of the off-gases to the pressure of the refinery fuel gas system, whilst the less volatile components can be dealt with in a lower pressure distillation system which will operate more efficiently than if this separation were done under high pressure conditions.
  • one of the primary innovations of the present invention is that two distillation towers or units are used, one being what we later refer to as the preflash distillation tower that operates at relatively high pressure to deal with the more volatile components at a temperature such that water cannot condense in the upper part of the tower with the subsequent low pressure distillation tower being used most efficiently to separate the less volatile constituents.
  • the crude oil feed is heated and then flashed in the preflash distillation tower, which operates with a flash zone pressure within the range of approximately 4.4 to 7.9 bar absolute (50 to about 100 psig).
  • the not readily condensible components as well as the LSR naphtha are taken as overhead products of the preflash distillation tower.
  • the top section of the high pressure preflash distillation tower is hotter than in conventional low pressure preflash systems and hence water condensation does not take place in the top section of this tower.
  • the overhead stream from the preflash distillation tower is further processed to separate sour water, LSR naphtha, and not-readily condensible components.
  • An intermediate naphtha side cut is withdrawn from the preflash distillation tower and stripped in a reboiled side-stripper to yield a heavy naphtha product.
  • the bottoms stream from the preflash distillation tower is heated and sent to an atmospheric crude tower and further processed to separate kerosene, diesel, atmospheric gas oils, reduced crude and small amounts of naphtha remaining in the bottoms stream in the high pressure preflash tower.
  • the load of the atmospheric crude tower is reduced considerably, resulting in a marked reduction in the diameter and height of that tower as well as a reduction in the duty of the heater required to heat the preflashed crude stream prior to feeding it to the flashzone of the atmospheric crude tower.
  • Figure 1 is a schematic diagram illustrating the crude oil component separation method of the present invention.
  • the components of crude oil are separated to produce streams of non-readily condensible compounds, LSR naphtha, heavy naphtha, and heavier compounds such as diesel, kerosene, atmospheric gas oils and reduced crude.
  • the crude oil feed may consist of any of the various mixtures of petroleum components that may be found in any type of crude oil.
  • FIG. 1 illustrates schematically the typical design of the method of the present invention.
  • a crude oil feed stream 8 is pumped in a crude oil feed pump 10 to a relatively high pressure.
  • the pressure will preferably be set such that any off-­gases ultimately obtained using the method of this invention will be obtained at a pressure equal to or higher than the pressure of a fuel gas system located downstream.
  • the crude oil feed stream 8 After the crude oil feed stream 8 is pumped, it is heated to a relatively high temperature using one or more heat exchangers 12 exchanging heat with one or more hot crude oil components. Typically, several heat exchangers 12 will be used. It should be noted that a fired heater can be substituted and/or added for any or all of the heat exchangers 12 and also that the method of the present invention is not affected by the scheme used to perform the heating step nor by performing the heating step prior to the pumping step.
  • the crude oil feed stream 8 contains an overabundance of volatile gases, it may be preferable to remove a portion or all of such gases prior to feeding the crude oil into the high pressure preflash tower.
  • a typical way to do this is to use a flash drum after a heating step to separate the more volatile gases as a vapor while retaining the less volatile component as a liquid.
  • the process of the present invention seeks to suppress vaporization during the initial heat up and pumping stages by means of a back pressure control valve 11 operated by a pressure control sensor 15 located immediately upstream of the preflash distillation tower.
  • the pumped and heated crude oil feed stream 9 is then fed to a preflash distillation tower 14 at an inlet 13.
  • the preflash distillation tower 14 can be any of conventional types of distillation towers designed to accommodate the operating conditions of such a preflash distillation tower.
  • the preflash distillation tower 14 is provided with stripping steam 16 at a point below the crude oil feed stream inlet 13.
  • exchangers 12 or the optional fired heater
  • a fired reboiler located below the crude oil feed stream inlet 13 at the bottom of the preflash tower 14.
  • the use of a feed heater and/or a reboiler will generally not be necessary unless the crude oil feed stream 8 has a larger than normal portion of naphtha components.
  • the crude oil feed stream 8 normally will contain 20 to 30 percent naphtha. If, however.
  • the preflash distillation tower 14, in accordance with the pressure objective discussed above, will typically operate within a range of about 4.4 to 7.9 bar absolute (50 to 100 psig) with a preferred range being about 6.2 to 6.9 bar absolute (75 to 85 psig).
  • the preflash distillation tower 14 has an overhead stream 18 which passes through one or more partial condensers 20 before being fed to an accumulator 22.
  • the partial condenser or condensers and accumulator form a partial condensing unit.
  • the accumulator 22 is a standard drum that also has means for separating sour water from the liquid petroleum condensate. Sour water is removed as a stream 24 and the liquid petroleum condensate from the accumulator 22 is refluxed to the top of the preflash distillation tower 14 in a stream 26.
  • the sour water condensed out contains hydrogen sulfide and other sulfur compounds that would be corrosive to the preflash distillation tower 14 if present there in liquid form.
  • the operating pressure of the preflash distillation tower 14 and the operating temperature and pressure of the crude oil feed stream 9 being fed to the crude oil feed stream inlet 13 determine the amount of hydrocarbon vapor leaving the preflash distillation tower 14 in stream 18 and the partial pressure of the water vapor present in that overhead stream.
  • the outlet temperature of partial condenser 20 can be controlled to produce a difference of at least 2.8°C (5°F) between the water dew point of the vapor from the top tray of the preflash distillation tower 14 and the returning reflux 26, the latter having the higher temperature. Due to this temperature control, no water condenses in the preflash distillation tower 14.
  • the vapor that is not condensed in the partial condenser or condensers 20, due to the temperature requirements needed to avoid any water condensation in the preflash distillation tower 14, is fed through a second set of one or more partial condensers 28 to a second accumulator 30.
  • This accumulator 30 is similar to the first accumulator 22 in that it has a means for separating out sour water in a stream 32.
  • the remaining liquid condensed is LSR naphtha and can be collected in a stream 34 that will meet the stringent ASTM specifications for LSR naphtha.
  • Vapors not condensed in the second partial condenser or condensers 28 will consist of non-readily condensible compounds that may be used as fuel gas. These vapors can be fed to a fuel gas system in a stream 36.
  • Stream 36 is controlled by a pressure control valve 38 that can be any of a wide variety of standard pressure control devices.
  • This pressure valve 38 will be controlled by a pressure control sensor 40 that measures the pressure in the top section of the preflash distillation tower 14.
  • the pressure control sensor 40 responds to pressure changes within the preflash distillation tower 14 and will cause the opening or closing of the pressure valve 38 to maintain the relatively high operating pressure throughout the system.
  • An intermediate side cut 42 is taken from the preflash distillation tower 14 at a point above the crude oil feed stream inlet 13. This intermediate side cut 42 is fed to a naphtha stripper column 44.
  • the naphtha stripper column 44 is a stripper column provided with a reboiler 46 that may be operated either by heat exchange with other process streams or by a heater.
  • the overhead from the naphtha stripper column 44 is returned to the preflash distillation tower 14 in a stream 48.
  • This vapor stream 48 will consist primarily of light components while the bottoms stream 50 of the naphtha stripper column 44 will contain heavy naphtha of such quality that it can meet the stringent ASTM specifications.
  • the naphtha stripper column 44 is equipped with a reboiler 46 because steam stripping would introduce water vapor that could once again result in the aforementioned water condensation problem.
  • the required duty of the naphtha stripper column reboiler 46 is a function of the number of trays in the naphtha stripper column 44, the sidestream feed composition and the specification of the heavy naphtha bottom product. In the preferred embodiment of the present invention, all of these interdependent variables are optimized.
  • more than one side-cut 42 may be taken from the preflash distillation tower 14 without affecting the method of the present invention.
  • the number of such side cuts will depend upon the operating conditions and the composition of the crude.
  • the bottoms stream 52 from the preflash distillation tower 14 contains primarily crude oil components heavier than heavy naphtha with small amounts of heavy naphtha and even smaller amounts of light naphtha. It is heated by heat exchange in one or more crude preheat exchangers 54 and/or a crude heater 56 such that all of the desirable components to be collected are vaporized (the heater generally being required because of the high temperature required downstream).
  • the stream is then fed to a low pressure atmospheric crude tower 58 at a stream inlet 62.
  • the atmospheric crude tower 58 may be any of a variety of well known low pressure crude towers.
  • the atmospheric crude tower 58 is provided with stripping steam 60 at a point lower than the stream inlet 62.
  • the bottoms stream 64 of the atmospheric crude tower 58 contains reduced crude oil, substantially free of naphtha, kerosene, diesel, atmospheric gas oils, or any of the lighter desirable components of crude oil. This bottoms stream 64 can be fed to a typical vacuum tower for further recovery of desirable heavy petroleum fractions.
  • the atmospheric crude tower 58 will typically operate at pressures ranging from about 1.34 to 3.41 bar absolute (5 to about 35 psig), resulting in a pressure of 1.34 to 2.03 bar absolute (5 to 15 psig) in the second stage accumulator 92, discussed below, the minimum pressures required to ensure adequate operation of the system.
  • the atmospheric crude tower 58 is usually equipped with a number of side-stream draw-off product strippers, of which a side cut kerosene stripper 66 as shown in Figure 1 is a typical example.
  • the side cut kerosene stripper 66 receives a side cut 68 from the atmospheric crude distillation tower 58 drawn-off from a point located above the bottoms stream inlet 62.
  • the side cut kerosene stripper 66 is provided with stripping steam through line 70, and a bottoms stream 72 of kerosene product can be collected.
  • the overhead stream 74 from the side cut kerosene stripper 66 is returned back to the atmospheric crude distillation tower 58 at a point higher than the side cut stream 68.
  • a pump around cooler 75 will be provided to remove heat and generate internal reflux in the atmospheric crude tower 58 in the vicinity of the kerosene stripper side cut 68.
  • the heat removed in such a pump around cooler 75 is used to preheat the incoming crude oil feedstream 8.
  • two or more additional side cuts and pump arounds can be taken below the kerosene side cut 68 and above the feed inlet 62 in a similar manner.
  • a preferred embodiment of the present invention is to allow those small amounts of naphtha to be recovered in the atmospheric crude tower overhead system where the heavy naphtha fraction is separated from the overhead stream 76 in a first stage accumulator 78.
  • the temperature in the first stage accumulator 78 is regulated by the use of one or more partial condensers 80 such that an LSR-free heavy naphtha condensate is produced in the first stage accumulator 78.
  • This LSR-free heavy naphtha condensate can be collected in a stream 82 that may be combined with the bottom stream 50 from the naphtha stripper column 44 to form a combined heavy naphtha product stream 84.
  • a portion of the heavy naphtha condensate stream 82 is refluxed to the atmospheric crude distillation tower 58 in a stream 86. It will be readily apparent to one of ordinary skill in the art, given the description and discussion herein, that it is not necessary to combine the heavy naphtha stream 82 with the bottoms stream 50 from the naphtha stripper column 44.
  • the naphtha components not condensed in the first stage partial condenser or condensers 80 leaves the first stage accumulator 78 as a vapor in stream 88.
  • One or more condensers 90 regulate the temperature of this vapor stream 88 such that it is condensed and collected in a second stage accumulator 92.
  • the condensed naphtha stream 94 leaves the second stage accumulator 92 is pumped in a pump 96 to a pressure somewhat higher than that of the naphtha stripper column 44, is heated in one or more heat exchangers 98 to its bubble point temperature, and is then fed to the top of the naphtha stripper column 44 at inlet 100.
  • the first stage accumulator 78 and the second stage accumulator 92 will preferably have means for separating the removing sour water in streams 102 and 104 respectively.
  • the LSR naphtha components are stripped out from the heavy naphtha, resulting in very good separation between the LSR naphtha and the heavy naphtha.
  • the conditions of the preflash distillation tower 14 might vary from a pressure of approximately 6.4 bar abso­lute (75 psig) and a temperature of 124°C (256°F) at the top tray to 6.5 bar absolute (80 psig) and 257°C (494°F) at the bottom tray, with pressure slightly higher than 6.5 bar absolute (80 psig) and a 267°C (513°F) temperature at the crude oil feed inlet.
  • the temperature of the first accumu­lator 22 of the overhead of the preflash distillation tower 14 may be 83°C (181°F) while the second accumulator 30 would operate at a pressure of 5.1 bar absolute (60 psig) and a temperature of 38°C (100°F), thereby condensing out high quality LSR naphtha.
  • the typical operating conditions discussed herein will vary depending upon the composition and type of crude charged to the system and upon various other conditions. The present example is only for illustration purposes.
  • the atmospheric crude tower 58 will typically oper­ate at conditions of about 1.7 bar absolute (10 psig) and 187°C (369°F) at the top tray to 2 bar absolute (15 psig) and 383°C (722°F) at the bottom tray.
  • a kerosene side cut stream 68 might be at 236°C (457°F) with the bottoms stream 72 from the side cut kerosene stripper 66 being at 227°C (440°F).
  • the first stage accumulator 78 of the overhead from the atmospheric crude tower 58 may operate at a temperature of 103°C (218°F) while the second stage accum­ulator 92 would operate at a pressure of 1.1 bar absolute (2 psig) and a temperature of 46°C (114°F).
  • Typical temperatures for the naphtha stripper column 44 are 173°C (343°F) at the top tray and 208°C (393°F) at the bottom.
  • the high pressure preflash distillation tower design solves some of the problems and efficiencies encountered in typical prior art designs.
  • the high pressure preflash distillation tower 14 enables the separation of the LSR naphtha from the heavy naphtha avoiding the use of a naphtha splitter, with its inherent condensing, vaporizing, and recondensing stages of naphtha components, and hence is more energy efficient.
  • Other advantages of this design are that the vapor feed load to the atmospheric crude tower 58 and the reflux requirements to produce acceptable grades of LSR and heavy naphtha are reduced considerably. This means that the atmospheric crude tower 58 can be designed smaller in diameter and significantly shorter in height.
  • the reduced load also means that the duty of the crude heater 56 can be significantly smaller.
  • the naphtha stripper column 44 is smaller than the corresponding naphtha splitter of the prior art. The reduced size and heat duty of each of these items leads to both capital cost and energy savings.
  • the overhead systems designs of both the atmospheric crude tower 58 and the preflash distillation tower 14 include multiple overhead accumulator/condensers. Advantages obtained from such a design are that water condensation can be avoided in the top sections of both of the towers and higher temperatures for the overhead condensers 20 and 80 can be utilized. The ability to use higher temperature overhead condensers gives the system more flexibility and allows for greater energy recovery.
  • Energy savings can also be realized downstream in that the higher bottoms temperature of the atmospheric crude tower 58 leads to reduced duty in the feed heater for the ensuing vacuum tower.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Fixed Capacitors And Capacitor Manufacturing Machines (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Claims (10)

1. Procédé pour la séparation des composants d'huile brute qui comprend l'apport d'un courant d'alimentation chauffé et pressurisé de l'huile brute à une tour de distillation fonctionnant à une température suffisamment élevée pour exclure une condensation d'eau à l'intérieur, la séparation du courant d'alimentation en un courant de tête contenant les composants les moins condensables, un courant de pied et un ou plusieurs courants latéraux contenant le naphte lourd, le courant latéral contenant le naphte lourd étant recueilli sur la tour à une sortie de courant latérale et étant fourni à une colonne de stripage, la vapeur de tête provenant de la colonne de stripage étant fournie à une entrée latérale de la tour, et le courant de pied de naphte étant recueilli au pied de la colonne de stripage, caractérisé par le fait que la tour fonctionne à une pression d'au moins 4,4 bars absolus (50 psig), le courant de tête comprenant la fraction naphte léger de première distillation de l'huile brute fournie, le courant de pied provenant de la tour est chauffé pour vaporiser les composants légers y contenus avant d'être fourni à une unité de distillation de brut fonctionnant à un pression relativement basse par rapport à la pression de fonctionnement de la tour de distillation et, sur une entrée placée plus haut qu'une entrée de vapeur sur l'unité de distillation, le courant de pied provenant de la tour est séparé, dans ladite unité de distillation, en composants comprenant un courant de pied de produit brut réduit et un courant de tête qui est fourni à une paire d'unités de condensation montées en série, la deuxième unité de condensation étant une unité de condensation totale et la première unité de condensation étant une unité de condensation partielle, au moins une partie d'un condensat de pétrole provenant de la première desdites unités de condensation est fournie à une entrée de reflux de tête de l'unité de distillation de brut, le reste dudit condensat de pétrole est recueilli sous forme d'un produit de naphte lourd, la vapeur provenant de la première de ladite paire d'unités de condensation est fournie à ladite deuxième unité de condensation, et un condensat de pétrole provenant de la deuxième unité de condensation est fourni à la colonne de stripage.
2. Procédé selon la revendication 1, caractérisé par le fait que la tour est maintenue à une pression comprise entre 4,4 et 7,9 bars absolus environ (50 et 100 psig).
3. Procédé selon la revendication 1, caractérisé par le fait que la tour est maintenue à une pression comprise entre 6,2 et 6,9 bars absolus environ (75 et 85 psig).
4. Procédé selon la revendication 1, 2 ou 3, caractérisé par le fait que l'huile brute chauffée est fournie à la tour à une pression comprise entre 4,4 et 7,9 bars absolus environ (50 et 100 psig).
5. Procédé selon la revendication 1, 2 ou 3, caractérisé par le fait que l'huile brute chauffée est fournie à la tour à une pression comprise entre 6,2 et 6,9 bars absolus environ (75 et 85 psig).
6. Procédé selon l'une quelconque des revendications précédentes, comprenant de plus les étapes consistant à :

Fournir le courant de tête provenant de ladite tour à une deuxième paire d'unités de condensation partielle montées en série

Fournir le condensat de pétrole provenant d'une première unité de condensation partielle de ladite deuxième paire à une entrée de reflux de la tour,

Fournir une vapeur provenant de la première unité de condensation partielle de ladite deuxième paire à la deuxième unité de condensation partielle de ladite deuxième paire,

Recueillir le condensat de pétrole provenant de la deuxième desdites unités de condensation partielle de ladite deuxième paire sous forme de naphte léger de première distillation, et

Fournir une vapeur provenant de la deuxième desdites unités de condensation partielle de ladite deuxième paire à un système à gaz combustible.
7. Procédé selon la revendication 6, caractérisé par le fait que la tour est maintenue à une pression supérieure à la pression du système à gaz combustible.
8. Procédé selon la revendication 6 ou 7, comprenant de plus l'étape consistant à séparer l'eau sulfureuse d'avec les condensats de pétrole dans chacune des unités de condensation de ladite deuxième paire d'unités de condensation partielle.
9. Procédé selon l'une quelconque des revendications précédentes, comprenant de plus l'étape consistant à séparer l'eau sulfureuse d'avec le condensat de pétrole dans chacune des unités de condensation de ladite paire d'unités de condensation.
10. Procédé selon l'une quelconque des revendications précédentes, comprenant de plus les étapes consistant à :

Recueillir les courants latéraux provenant de l'unité de distillation de brut en des points placés au-dessus de l'entrée d'alimentation de ladite unité de distillation de brut,

Fournir ces courants latéraux provenant de l'unité de distillation de brut à une ou plusieurs colonnes de stripage de produit de courant latéral,

Fournir les têtes provenant de ces colonnes de stripage de produit de courant latéral, à des entrées de courant latéral de l'unité de distillation de brut placées en des points se trouvant au-dessus de l'entrée d'alimentation de brut de ladite unité de distillation de brut, et,

Recueillir un courant de pied provenant de chacune de ces colonnes de stripage de produit de courant latéral sous forme de produits de pétrole.
EP86306043A 1985-08-23 1986-08-05 Procédé pour la séparation d'huile brute Expired - Lifetime EP0213791B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US06/768,615 US4673490A (en) 1985-08-23 1985-08-23 Process for separating crude oil components
US768615 1985-08-23

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EP0213791A2 EP0213791A2 (fr) 1987-03-11
EP0213791A3 EP0213791A3 (en) 1988-08-31
EP0213791B1 true EP0213791B1 (fr) 1991-01-02

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US (1) US4673490A (fr)
EP (1) EP0213791B1 (fr)
DE (1) DE3676392D1 (fr)
NO (1) NO169903C (fr)

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WO2002049735A1 (fr) * 2000-12-20 2002-06-27 Gosfern Pty Limited Appareil et procede de conditionnement de petrole brut

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EP0213791A2 (fr) 1987-03-11
NO169903C (no) 1992-08-19
NO863366L (no) 1987-02-24
DE3676392D1 (de) 1991-02-07
EP0213791A3 (en) 1988-08-31
US4673490A (en) 1987-06-16
NO863366D0 (no) 1986-08-21

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